Power generation methods and systems

ABSTRACT

Thermodynamic energy methods and systems that provides all electrical energy and heat needs of a single residential house, commercial business or office building. The system is small enough to be stored inside the house or building. The system can generate excess electrical energy which can be sold over a power grid and allow for the house owner, building owner or energy provider (utility company) to provide income. The method and system can have combined energy conversion efficiency up to approximately 97%. Components can include amorphous materials, and the mono-tube steam generator boiler which is explosion proof when punctured, and only emits a puff of steam when punctured. The tubes can be built to pressure vessel code. The invention can use steam generators to power A/C units, domestic hot water, hot water air space heaters, other loads such as pools and spas and underground piping to eliminate ice and snow. Additionally, the invention can be used to power vehicles such as cars, and the like. Other embodiments can use thermodynamic energy methods and systems that provides electrical energy and heat needs of a residence, commercial business, or office building, that include supertropically expanding ammonia vapor against a vacuum, as generated by chemosorption, in order to convert moderate amounts of heat into mechanical energy at high efficiencies. A supertropic package system can include a source of ammonia/water, a thermal generator for heating the source of ammonia/water and generating ammonia gas, a positive displacement device for expanding the gas, and generating electricity from a power source driven by the expander.

This is a continuation of pending application Ser. No. 10/826,652, filedApr. 16, 2004 which claims the benefit of priority to U.S. ProvisionalApplication 60/544,466, and this invention is a Continuation-In-Part ofU.S. patent application Ser. No. 10/414,672 filed Apr. 16, 2003, whichclaims the benefit of priority to U.S. Provisional Application Ser. No.60/372,869 filed Apr. 16, 2002, the disclosures of which areincorporated by reference herein.

FIELD OF INVENTION

This invention relates to energy generation and power supply systems,and in particular to methods and systems that can meet all energydemands of a home or business or industrial use, and allows for excesselectrical energy to be available to be sold over transmission grids,and in particular to expansive fluid systems and methods such as steamgeneration for generating electrical energy, and using co-generated heatbyproducts for domestic hot water, room heating and swimming pool/spaheating, and for powering air conditioners and vehicles, and also toexpansive methods and systems that use supertrope power packs forcondensing vapor such as ammonia gas to condense and convertingresulting energy into generated electrical power.

BACKGROUND AND PRIOR ART

Endpoint Power Production

Many problems currently exist for traditional power generation methodsand systems. Approximately 95% of the current world's supply ofelectrical energy is produced from non-renewable sources. Alternativefuels are not practical sources for taking care of all the world'selectrical energy needs. For example, solar energy power is too low, notreliable and very expensive. Wind energy is inconsistent, notdependable, expensive, and high maintenance. Geothermal energy requiresspecific locations to be used. Hydrogen energy has no existinginfrastructure to support, distribution.

Global energy demand is increasing at approximately 2% per year. TheDepartment of Energy has forecast by year 2020 that United States willneed approximately 403 gigawatts (403 billion watts) and the world willneed approximately 3,500 gigawatts (3.5 trillion watts of power). Still,there are more than two billion people in the world who do not haveaccess to electricity.

Demand for electricity is outrunning capacity, and the price mechanismis the essential way to restrain demand and encourage supply. Therefore,the cost of electricity will keep going up.

Current electric utility companies are limited by production capacity toincrease their electricity generation. To increase generation, thesecompanies must build additional plants which require substantial capitalinvestments, political issues of where to locate to the plants, lengthypermit procedures lasting several years, cost overruns, which make thetraditional method of building additional plants undesirable.

Using nuclear power, oil burning plants, and coal burning plants, addsfurther environmental problems for those seeking to build electricitygenerating power plants. Thus, building more and more plants is not apractical solution.

Current energy conversion efficiency of any of these power plants isgenerally no higher than 30% (thirty percent) efficiency of theelectricity produced from the energy source of the fuel (oil, coal,nuclear, natural gas). For example, turbines that generate theelectricity from the fuel source at the power plants only generate up toapproximately 30% efficiency of the electricity generated from thesource.

Next, the electricity being transmitted loses efficiency while it isbeing transmitted loses energy (efficiency) over transmission lines(i.e. wires, substations, transformers) so that by the time theelectricity reaches the end user, an additional 28% (twenty eightpercent) energy (efficiency) is lost. By the time the electricityreaches an end user such as a home residence, the true energy efficiencyis no more than approximately 18% (eighteen percent) from the actualenergy source.

Co-generation heat is the amount of heat that is wasted in thedevelopment of the electric power at the plant because heat cannot betransmitted over long distances.

A co-generation combined system does exist where some of theco-generated heat produced from a gas fired plant is used to produceadditional steam which then makes additional electricity in addition tothe primary electrical generation system. This combined system canachieve up to approximately 45% (forty five percent) energy conversionefficiency. But there still are transmission losses of some 28% (twentyeight percent) so that by the time electricity reaches the end user onlysome 22% (twenty two percent) of the actual energy source is convertedto electrical power.

The current electricity rate structure for consumers penalizes theconsumers who must pay for the fuel being used to generate either 18percent or 22 percent energy conversion efficiency. In essence, theconsumer is paying for some 500% (five hundred percent) of the actualcost of electricity by inherent transmission losses that are generatedby the current power generation systems.

The inventors are aware of several patents used for steam powergeneration. See for example, U.S. Pat. No. 3,567,952 to Doland; U.S.Pat. No. 3,724,212 to Bell; U.S. Pat. No. 3,830,063 to Morgan; U.S. Pat.No. 3,974,644 to Martz et al.; U.S. Pat. No. 4,031,404 to Martz et al.;U.S. Pat. No. 4,479,354 to Cosby; U.S. Pat. No. 4,920,276 to Tateishi etal.; U.S. Pat. No. 5,497,624 to Amir et al.; U.S. Pat. No. 5,950,418 toLott et al.; and U.S. Pat. No. 6,422,017 to Basily. However, none ofthese patents solves all the problems of the wasteful energy conversionmethods and systems currently being used.

Nonexistence of Supertropic Expansion Applications

At present, known thermodynamic changes of conditions of a system do notinclude supertropic expansion, which is defined as extracting moreenergy from an expanding gas, than what isentropic expansion gives for agiven expansion volume ratio. In this way a vapor can be expanded farinto the wet area of its ph-diagram, so a considerable amount of itcondenses by doing work, instead of by cooling it to ambient waste.

Currently, it is not possible to convert moderate amounts of heat fromexternal sources into mechanical energy. Steam turbines work on highrotational speeds that increase to impractical values when the machineis scaled down in size. Thus steam turbine sizes range in the megawatts.

Smaller displacement steam expanders would have a too low efficiency.The only alternative external combustion engine in the range of up to afew hundred kilowatts would be the Sterling engine, but it cannot beproduced at a compatible cost in relation to internal combustionengines. Besides, as it only works on the specific heat of an inert gasover varying temperatures, the size of a Sterling engine potentially ismuch larger than for an according steam, or internal combustion engineand so it must work on very high pressure levels to increase the mass ofgas contained in the cycle and thus to keep the machine size down.Again, leakage sets the technological limits, though likely economicones do sooner.

A basic patent that issued to James Watt on Jul. 17, 1782 was anexceedingly important one, and of special interest in the history of thedevelopment of the economical application of steam. This patentincluded: 1. The expansion of steam, and six methods of applying theprinciple and of equalizing the expansive power. 2. The double-actionsteam-engine, in which the steam acts on each side of the pistonalternately, the opposite side being in communication with thecondenser.

FIG. 18 shows the progressive variation of pressure (of the volume jabove the piston) as expansion proceeds. It is seen that the work doneper unit of volume of steam as taken from the boiler, is much greaterthat when working without expansion. The product of the mean pressure bythe volume of the cylinder is less, but the quotient obtained bydividing this quantity by the volume or weight of steam taken from theboiler, is much greater with, than without expansion. Watt specified acut-off at one-quarter stroke, after which the steam expands theremaining three-quarters, as usually best. This would do a little morethan double the effect, but it would too much enlarge the cylinder andvessels to use it all.

It was found that for the case assumed and illustrated here, the workdone during expansion per pound of steam is 2.4 times that done withoutexpansion. This indicated that Watt measured supertropic expansion,because otherwise the work ratio would have been slightly over two, asfollows: Lets imagine a cylinder with 1 m2 area (One square meter) and a4 meter stroke length, thus consuming 4 m3 (Four cubic meters) steam ofatmospheric pressure under full load per stroke and at 0.25 barcondenser pressure, giving 0.75 bar constant pressure difference overthe piston. The work done would then be approximately 75 kappa×4m=approximately 300 kJ. With a specific volume of approximately 1.7m3/kg for the applied steam, we get a specific work of approximately 128kJ/kg.

As previously mentioned, the inventors are not aware of patents thatsolve all the problems of the wasteful energy conversion methods andsystems currently being used.

SUMMARY OF THE INVENTION

Endpoint Power Production Objectives

A primary objective of the invention is to provide a more efficientmethod and system to generate electrical power and heat to supplyindividual homeowners and businesses to make them independent of thetraditional electrical company at a much lower cost/efficiency.

A secondary objective of the invention is to provide a method and systemto generate electrical power that provides for all the energy needs tosupply electricity, hot water, heating and cooling for individualhomeowners and businesses.

A third objective of the invention is to provide a method and system togenerate electrical power and heat energy for the needs of individualhomeowners and businesses, that allows for their excess energy to besold to others further reducing costs to homeowners and businesses.Current estimates would allow for selling approximately $10,000 toapproximately $22,000 per year worth of excess energy to others throughan existing electrical power grid.

A fourth objective of the invention is to provide a method and system togenerate electrical power to supply all the energy needs of individualhomeowners and businesses that is inexpensive. An estimated cost of thenovel invention system would be under $10,000 for the entire system.

A fifth objective of the invention is to provide a method and system togenerate electrical power and heat that can reduce national energyresidential energy consumption substantially over current levels.

A sixth objective of the invention is to provide a method and system togenerate electrical power and heat that reduces United States dependencyon foreign sources of energy such as oil imports.

A seventh objective of the invention is to provide a method and systemto generate electrical power and heat that can use any energy sourcesuch as renewable (alcohol, hydrogen, etc) and non renewable (oil, coal,gas, etc.) in an efficient energy conversion method and system.

An eighth objective of the invention is to provide a method and systemto generate electrical power and heat that achieves an energy conversionefficiency of approximately 95% (ninety five percent) or greater.

A ninth objective of the invention is to provide a method and system togenerate electrical power and heat that does not charge the end user forfuel source energy that is being lost and not being used to generate theactual electricity.

A tenth objective of the invention is to provide a method and system togenerate electrical power and heat that can use existing powergeneration infrastructures such as existing natural gas pipelines,propane gas tanks, and the like.

An eleventh objective of the invention is to provide a method and systemto generate electrical power and heat that does not require building newplants, substantial capital expenditures, permitting costs, lesspolitical headaches of where to locate plants, and the like.

A twelfth objective of the invention is to provide a method and systemto use superheated steam generated by a vaporous fuel source to supplyhot water for uses such as but not limited to domestic hot water,home/space heating, and other loads such as pools, spas, and undergroundpiping for ice and snow removal.

A thirteenth objective of the invention is to provide a method andsystem to use superheated steam generated by a vaporous fuel source topower an air conditioning unit.

A fourteenth objective of the invention is to provide a method andsystem to use superheated steam generated by a vaporous fuel source togenerate electricity for powering commercial and domestic devices.

A fifteenth objective of the invention is to provide a method and systemto use superheated steam generated by a vaporous fuel source to power avehicle such as a car.

Supertropic Power Production Objectives

A sixteenth objective of the invention is to provide a more efficientmethod and system to generate electrical power from heat by achieving amode of a expansion, called “supertropic”, that causes the major part ofthe mass of vapor to condense and convert the according energy intomechanical power.

A seventeenth objective of the invention is to provide methods andsystems of using supertropic expansion power packs to generateelectrical power for power grids.

An eighteenth objective of the invention is to provide methods andsystems of using supertropic expansion power packs to generateelectrical power for powering vehicles, such as cars.

A nineteenth objective of the invention is to provide methods andsystems of using supertropic expansion power packs to generateelectrical power to generate electricity for powering commercial anddomestic devices.

Endpoint Power Production Embodiments

The invention can use any potential source of energy, such as renewableand nonrenewable energy, such as but not limited to natural gas, liquidpropane gas, and the like, and the invention can run on coal, oil or anyfuel that can be vaporized. The invention can also be made to run onwater; thru the use of advanced techniques (blue laser, electrolysis) ofbreaking the bi-polar bond of H₂O and uses the gasses H₂ and O₂.

A preferred embodiment can have simple and user friendly automatedcontrols controlled by computers and software, that can monitor andcontrol the entire system. The size of the system can be no larger thanapproximately 3 feet by 4 feet by 5 feet, and weigh no more thanapproximately 500 pounds, and have an almost silent operation. The novelinvention can meet the minimum energy needs of a residential home orbusiness.

At a maximum mode, the embodiments can additionally supply excesselectrical energy to sell over a transmission grid, which can generateextra income for the user that can be in the range of approximately$10,000 to approximately $22,000 per year, which can easily pay back thecosts to buy the system. The embodiments are scalable and can be builtto produce power levels of approximately 20 KW, 30 KW, or more.

Other embodiments of the invention use superheated steam generated froma vaporous fuel source to power electric and shaft driven airconditioning units, vehicles such as cars, and the like.

Supertropic Power Production Embodiments

Supertropic Expansion can be defined as extracting more energy from anexpanding gas than what isentropic expansion will give (for a givenexpansion volumne ratio). In this way a vapor can be expanded far intothe wet area of its energy state, so that a considerable amount of thegas condenses from a vapor by doing work instead of just cooling toambient temperature as a loss. The invention in achieving greaterexpansion is to provide a vacuum generated by the process ofchemosorption of ammonia and water. Ammonia can be a new working fluid,and the water can be part of the chemosorption process.

The inventors have found a way to make the working fluid expand to amuch greater extent for a given volume, thereby releasing up toapproximately three times or more the energy to do work. An additionalbenefit of this approach is lowering operating pressures andtemperatures.

The chemosorption hardware can include 1) working fluid, 2) Absorber, 3)Desorber, 4) Receiver, 5) Regenerator, 6) Low volume pump.

In operation, the working fluid is heated in the Thermal Generator (TG),enters the invention as a gas, is then expanded Supertropically,delivering power to drive the electric generator (GEN). The gas, asenergy, is released, then condensed back into a liquid. The liquid thencontinues through the absorber, regenerator and desorber in a closedcycle to continuously provide a vacuum condition for SupertropicExpansion to take place.

Preferred embodiments include methods and systems that achieve a mode ofexpansion of a vapor, called “supertropic”, that causes the major partof the mass of vapor to condense and convert the according energy intomechanical power.

Novel methods and systems can be used for converting moderate amounts ofheat into mechanical energy at high efficiencies, by supertropicallyexpanding a gas vapor such as ammonia, and the like, against a vacuum,as generated by chemosorption, in order to convert moderate amounts ofheat into mechanical energy at high efficiencies. A

Preferred embodiments of a supertropic energy generating package system,can include a gaseous source such as but not limited to ammonia andwater, a thermal generator for heating the source of ammonia/water andgenerating a gas, a scroll expander for expanding the gas, and anelectricity generating power source, such as a motor/alternator beingdriven by the expanding gas.

Further objectives and advantages of this invention will be apparentfrom the following detailed description of the presently preferredembodiments which are illustrated schematically in the accompanyingdrawings.

BRIEF DESCRIPTION OF THE FIGURES

Endpoint Power Production

FIG. 1 is an overview diagram of a first preferred embodiment of theinvention.

FIG. 2A is a cross-sectional view of a first version heat generator(boiler) for the embodiment of FIG. 1, and can be used for compactspaces when space restricts height dimensions of a boiler of a doublecoil embodiment.

FIG. 2B shows a cross-sectional view of a single wrap fin coil heatexchanger (boiler) for the embodiment of FIG. 1 that can be used whereheight restrictions are not a problem.

FIG. 3 shows the heat recovery unit for the embodiment of FIG. 1.

FIG. 4 shows air preheater component for the embodiment of FIG. 1.

FIG. 5A is a perspective view of an expander driver for the embodimentof FIG. 1.

FIG. 5B is an exploded view of the expander driver of FIG. 5A.

FIG. 6 is a cross-sectional view of the expander driver of FIG. 5A alongarrows 6X.

FIG. 7 shows the steam to water exchanger (Co Generation Steamcondenser) for the embodiment of FIG. 1.

FIG. 8A shows the steam dissipation coil (heat dump steam condenser) forthe embodiment of FIG. 1.

FIG. 8B is an end view of the coil and fan assembly of FIG. 8A.

FIG. 9A shows the condensate return pump (high pressure return pump) forthe embodiment of FIG. 1.

FIG. 10B is a cross-section of the novel rifled and turbulator tubingused in the A/C unit 19 of FIG. 1.

FIG. 11 shows a wiring diagram for various components for FIG. 1.

FIG. 12 shows a preferred layout of all the components of the inventionin a 3′ by 4′ by 5′ box for use by the end user of the invention.

FIG. 13 shows a second preferred embodiment for heat generation using aclosed loop steam generator system.

FIG. 14 shows a third preferred embodiment for powering a drive shaftdriven air-conditioner unit using the novel steam generator, expanderand steam condenser of the invention, which is a vaporous fuel suppliedair conditioner

FIG. 15 shows a fourth preferred embodiment for supplying electricity toany electrically powered device or system using the novel steamgenerator, expander and steam condenser of the invention.

FIG. 16 shows a fifth preferred embodiment for supplying electricalpower to an electric vehicle, such as an electric car using the novelsteam generator, expander and steam condenser of the invention.

FIG. 17 shows a sixth preferred embodiment for powering a drive shaftdriven vehicle using the novel steam generator, expander and steamcondenser of the invention.

Supertropic Power Production

FIG. 18 shows a prior art view of the progressive variation of pressure(of the volume) above a piston in a steam engine.

FIG. 19A is a pressure volume graph of temperature versus entropy forsupertropic expansion.

FIG. 19B shows a pressure versus Enthalpy graph for the invention.

FIG. 20 shows an operational arrangement configuration for a supertropepower system.

FIG. 21 shows an energy balance diagram for the supertrope power systemof the invention.

FIG. 22 shows another version of the supertropic power system of FIGS.20-21 with a gas/air mixture heat source and superheator based on forcedgas/air combustion.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

Before explaining the disclosed embodiments of the present invention indetail it is to be understood that the invention is not limited in itsapplication to the details of the particular arrangements shown sincethe invention is capable of other embodiments. Also, the terminologyused herein is for the purpose of description and not of limitation.

Enpoint Power Production Embodiments

FIG. 1 is a flow chart diagram of a preferred embodiment system of theinvention. Initially, ambient air coming through an air preheater (1FIG. 1, shown in FIG. 4). The heated air is mixed with natural gas orpropane in the airblower/valve assembly 2 FIG. 1 (such as but notlimited to an AMETEK Variable Speed Power Burner Blower, or EBM, withgas metering devices such as those manufactured by Honeywell and CarlDungs, and the like. The airblower/valve assembly 2 supplies the airrequired for the combustion process from a primary fuel source 22. Theforced air blower can be sized based on the application and/orrequirements of the heat generator 3 FIG. 1. The gas metering portion ofthe airblower/valve assembly 2 provides the gaseous fuel (natural gas,propane, and the like.) required for the combustion process. This devicecan regulate the amount of gaseous fuel to provide the optimum stoicmetric air to fuel ratio (e.g. for natural gas, that ratio isapproximately 10 to approximately 1). The gaseous fuel enters the forcedair stream through the device. Alternative fuels can be used as a backup fuel source 23, if the current fuel supply is disrupted. The devicecan automatically shift to the back up source 23, such as but notlimited to propane tanks, by switching to a different orifice and otheradjustments which can automatically occur.

The invention can incorporate the latest in modulating blower, valve 2and burner technology in heat generator (boiler) 3. This allows theproper air/gas mixture at all inputs determined by a feedback signalfrom the electric load placed on the electric generator 9.

The proper gas air mixture (approximately 10 air to approximately 1 gas)is injected by blower 2 (a combination air blower fan and gas meteringdevice) into a burner inside the heat generator unit (boiler) 3 FIG. 1(shown in FIGS. 2A and 2B). Heated combusted gases heats the incomingwater from the closed loop system (12, 11, 7, 5, 6, 4 FIG. 1). Exhaustedflue gasses from boiler 3 pass through heat recovery 4 FIG. 1 (shown inFIG. 3), after heating incoming air exhausts into the atmosphere.

Steam generated in boiler (heat generator) 3 FIG. 1 (FIG. 2A or 2B) at atemperature of approximately 1000 F and approximately 600 PSI entersexpander 8 FIG. 1 (FIGS. 5A, 5B and 6). This steam in expander 8 causesa shaft 8SH in the expander to turn, the shaft SH is connected toelectric generator 9 FIG. 1 (FIG. 11). Electric generator 9 can be acommercial off the shelf generator (COTS) such as Lite Engineering Inc.,Marathon, e-Cycle. A preferred generator 9 can be a 240 Volt three-phaseAC power supply, or 120 Volt single phase AC power supply, and the like.

Referring to FIG. 1, electricity produced goes through a powerconditioning unit 17 FIG. 1 such as those commercial off the shelf unitsthat come with the electric generator 9 previously described to be putin proper phase and frequency for generation into an electrical powergrid 18 FIG. 1. Electric power grid 18 can be an existing grid thatsupplies electrical power to commercial, industrial and residentialapplications, such as but not limited to FPL (Florida Power and Light)electric power supply grid. Also, electricity generated out of powerconditioning unit 17 powers air conditioner 19 FIG. 1 (FIGS. 10A-10B).The power conditioning unit 17, can be an off-the-shelf unitmanufactured by Lite Engineering Inc. which adjusts parameters such asphase and harmonics coming out of electric generator 9 and such as astandard AC to DC type converter, and the like.

Heat dissipating units 20, 21 can consist of liquid pump and fan 21 andstandard heat exchanger (for example, a radiator, tubes with fins, andthe like) 20, which cools off generator 9 FIG. 1 and keeps generator ata temperature of approximately 130 F or less. Pump portion 21 can be afractional horsepower circulator of an anti-freeze solution, such asthose manufactured by TACO, Grundfos, and the like. Fan portion 21 canbe a pancake style blower of approximately 50 CFM (cubic feet perminute) operating at approximately 115 volts such as one manufactured byEBM, and the like. A heat sensitive speed controller (thermostat) suchas one manufactured by Honeywell, and the like, can be built into thefan portion, to operate the fan.

Co Generation Loop.

From Expander 8 FIG. 1 (FIGS. 5A, 5B and 6), the steam exhausted goes toa steam to water exchanger 10 FIG. 11 (FIG. 7) to a pump 14 (Off theshelf water circulator) to a domestic water heater 15, to hot water airheating coil 16 such as a room/house hot water space heater (a coilpassing through a fan, to other loads 13, such as but not limited to aswimming pool, a spa, underground pipes for ice and snow removal, andthe like. Next, the same hot water passes back at a reduced temperatureof up to approximately 30 F, to heat exchanger 10 FIG. 1 (FIG. 7). Whenco generation loop is completely satisfied (i.e. all the hot water isheated up in domestic water heater 15, no more heat is required forheating house 16, pool/spa is at desired temperature) then in order todissipate this excess heat, it passes from heat exchanger 10 to steamdissipation coil 11 FIG. 1 (FIGS. 8A-8B), where condensed water isplaced into accumulator 7 (water storage tank) by way of dissipationcoil vent check valve, which relieves built up vapor. Then, the highpressure condensate return pump 5 FIG. 1 (FIG. 9) pumps water to checkvalve 6 (keeps water from going backward). Pump 5 can run atapproximately 600 to approximately 1000 psi. Water is then passed toheat recovery unit (reclaimer) 4 FIG. 1 (FIG. 3). Water can be heated inrecovery unit (reclaimer) 4 and is pumped by a high pressure pump 5 intosteam generator (boiler) 3 for heating back into steam to complete thecycle of the entire system, where heat generator (boiler) 3 can operateat a temperature of approximately 1000 F to approximately 1,500 F.

In the cogeneration loop of FIG. 1, steam exits the expander drive 8 ata temperature at approximately 212 F to approximately 230 F. This steampasses through the steam to water exchanger 10 (FIG. 7), such as but notlimited to a Alfa Laval CB-14 a COTS item to extract the heat of thesteam and transfer it to the co generated water to be used for domestichot water, heating water to be used for domestic hot water 15 forheating water and other water usages 13 such as but not limited topools, snow melting, and the like. This co generated water is pumped bya COTS circulator pump 14, such as but not limited to a Taco or Grundfospump, and the like. In a situation where all co generated usages aresatisfied the excess heat (steam) continues on to the heat dissipationcoil 11, such as one manufactured by Heatcraft or other steam condensermanufacturers.

The condensed steam is now changed to water which gave up its latentheat to the co generated water. The closed loop steam, now water, istransferred to the accumulator 7 directly bypassing check valve ready tobe returned to the heat generator 3 by the high pressure bellows pump 5(FIG. 9).

FIG. 2A is a cross-sectional view of a first version heat generator(boiler) for the embodiment of FIG. 1, and can be used for compactspaces when space restricts height dimensions of a boiler. Air blower (2FIG. 1) forces an air/gas fuel mixture to enter burner. Gas/fuel meterin blower/meter 2 (FIG. 1) provides the gaseous fuel (natural gas,propane, and the like) from primary fuel source 22 (FIG. 1) required forthe combustion process. This device will regulate the amount of gaseousfuel to provide the optimum stoic metric air to fuel ratio (e.g. fornatural gas, that ratio is 10 to 1). The gaseous fuel enters the forcedair stream. Alternative fuels from a backup fuel source 23 (FIG. 1) canbe used as a back up if the current fuel supply is disrupted. The devicecan automatically shift to the back up source 23, such as but notlimited to propane tanks, by switching to a different orifice and otheradjustments can be made automatically.

The burner screens 302, 304 located inside the body of the heatgenerator 3, is where the fuel and air mixture is ignited and burned.The burner 305 consists of two cylindrical (inner and outer) screens302, 304. The purpose of the dual screens 302, 304 is to preventflashbacks from the combustion of the fuel and air mixture. The screens302, 304 can be made of Inconel or other high temperature materials, andthe like.

Referring to FIG. 2A, heat exchanger (double wrapped tubes 310) arewrapped around the burner 305 and can be constructed of approximately ⅝″321 stainless steel tubing with external outwardly protruding fins 315.The working fluid (water) is pumped through the heat exchanger (b pump 5FIG. 1, 9 at approximately 600 to approximately 1000 psi), where it isheated from an approximately 150° F. entering temperature to a leavingtemperature of approximately 1000 to approximately 1300° F. (nominal,approximately 1500° F. maximum) at approximately 1000 PSI. Once theworking fluid is heated it will then go to the expander drive 8 (FIGS.5A, 5B and 6).

An electrically powered igniter module 320 attached to the heatgenerator 3 adjacent to air/gas inlet line 301 can provide the necessaryenergy (spark) to start the combustion process. The insulation 325within heat generator housing 330 retains the heat that is generatedduring the combustion of the fuel and air mixture within the heatgenerator cavity to maximize the heat transfer to the heat exchanger(wrapped tubes 310). The insulation 325 can be composed of aluminum andsilica or other high performance insulation, and the like. Exteriorouter generator housing 330 can be composed of stainless steel,aluminum, high temperature plastic, and the like, and houses theinsulation 325, heat exchanger 310, and burner screens 302, 304.

A downwardly extending flue 340 exhausts the products of combustion(flue gases). The flue gases, which are very friendly to the environmentare primarily carbon dioxide and water vapor with trace amounts (ppm) ofCO. A minimal amount of heat (≦ approximately 2% of total heatgenerated) is also lost through the flue. The flue gases can beharmlessly exhausted to the atmosphere.

Water entering heat generator (boiler) 3 FIG. 1, FIG. 2A from heatrecovery (reclaimer 4 FIG. 1) is pumped to flow through the doublewrapped finned coiled heat exchanger tubes 310, and exits the boiler atapproximately 1000 F to approximately 1500 F to pass to the expanderdrive 8 FIGS. 1, 5A, 5B and 6.

FIG. 2B shows a cross-sectional view of a single wrap fin coil heatexchanger (boiler) 3′ for the embodiment of FIG. 1 that can be usedwhere height restrictions are not a problem. In FIG. 2B, a plug 350 suchas a high temperature insulation material previously described ispositioned below a burner, and is used for directing the forced aircombustion against the exterior fins on the single layer of wrapped fincovered coil tubes 310′. The upper end 355 of the plug 350 can bechamfered/taperered, and can be conical, and the like. Air swirls andturbulates about the fins 315′ which are about the coil tubes 310′ tomaximize heat transfer from the burner 305 to the water circulatingthrough the coils 310′. The other components in FIG. 2B functionsimilarly to those described in reference to FIG. 2A.

The heat generators 3 and 3′ of FIGS. 2A-2B produce steam to providemotive power to the system expander. FIG. 2A uses a mono-tube 310wrapped about it itself, and FIG. 2B is a single wrap mono-tube 310′.The mono-tube 310/310′, has a very small fluid capacity (0.64 gallons ofdistilled water). Any leakage would release the steam without anyexplosive power and therefore is a safe device even at the operatingpressure of approximately 600 to approximately 1000 psi and temperaturesof approximately 1000 to approximately 1300 F with a maximum ofapproximately 1500 F. The pressure drop would immediately shut off fuelsupply and stop the system operation.

The forced combustion blower and a modulating gas valve 2 FIG. 1, arecontrolled by the ignition module 320 in FIGS. 2A-2B, which delivers amixture of fuel gas and air to the burners 305 within the heat generator(boiler) 3, 3′ of FIGS. 2A, 2B. The burner 305 can be one manufacturedby Burner Systems Inc. or Cleveland Wire Cloth, where the combustiontakes place on the burner surface 302, 304 to heat the water to steam inthe heat generator tubes 310, 310′.

The tubes 310, 310′ in the heat generators 3, 3′ of FIGS. 2A-2B caninclude approximately 0.018, approximately 321 stainless steel finmaterial of approximately 0.125 and approximately 0.25 height wrappedand brazed around at approximately 14 to approximately 11 fins per inch.An approximate 0.625 ID (internal diameter), approximate 321 stainlesssteel tube of approximately 0.083 wall as required to meet the requiredpressure vessel codes.

Referring to FIGS. 2A-2B, heat can be absorbed by the helix (helical)coil tubes 310, 310′ from radiation from the burner flame in burner 305and from convection of the products of combustion of forced combustionburner 305, to produce output steam flow rate of approximately 95 poundsper hour at approximately 600 psi and approximately 1000 F.

Water in the heating coils 310, 310′ can be heated through the saturatedsteam range into the superheated steam range realm all in one heatgenerating path as opposed to standard methods using two stage steamsystems with a separate super heat section.

FIG. 3 shows the heat recovery unit (liquid condensate heat exchanger) 4for the embodiment of FIG. 1. Flue gas from bottom extending flue 340passes into a chamber having double wrapped mono-tube finned 410 heatexchanger, and maximizes heat efficiency to water passing through thedouble wrapped tubes 410 within a housing 430 (similar in material tothe housing 330 of the heat generator 3. The Liquid Condensate HeatExchanger (Reclaimer) 4 captures waste heat in the flue 340, which addsto the overall efficiency of the invention. This heat exchanger 4 can beconstructed of approximately 321 C stainless steel tubing 410 withexternal fins 415.

The flue heat reclaimer 4 in FIG. 3 captures heat from the flue gasexhaust to raise the temperature of the water from the steam condenser10 FIG. 1 before it is pumped by the high pressure pump 5 FIG. 1 intothe heat generator 3 FIG. 1.

Built of the same materials as the heat generator 3 FIG. 1 and able towithstand the pressure that exists in the heat generator 3: a spiralbaffle 450 can be used to distribute the flue heat to all the tubes 410for proper heat transfer.

FIG. 4 shows air preheater component 1 for the embodiment of FIG. 1. Acombustion air pre-heater increases the efficiency of the combustionburner 205 of FIGS. 2A, 2B by capturing the heat usually wasted in theflue 440, 140. Energy needed to heat the air in combustion is lowered,increasing the efficiency of the overall system. The pre-heater 110 canbe made of stainless steel materials for long life. Ambient air can bepulled into an opening 115 in the annular chamber 110 surrounding theflue 440, 140, by a combination fan/blower and gas meter 2 FIG. 1pulling the heated air out of opening 125 to be directed into the heatgenerator (boiler) 3 FIG. 1.

FIG. 5A is a perspective view of an expander driver 8 for the embodimentof FIG. 1. FIG. 5B is an exploded view of the expander driver of FIG.5A. FIG. 6 is a cross-sectional view of the expander driver of FIG. 5Aalong arrows 6X.

The expander drive 8 converts the thermal energy of the working fluidinto mechanical (rotational) energy to drive the generator or any othermechanical device.

FIGS. 5A, 5B and 6 show an expander drive system based Scroll Labs“floating scroll” technology (see U.S. patent Ser. No. 10/342,954 to oneof the inventors of the subject invention, which is incorporated byreference) for the subject invention. The scroll device 8, used ascompressors, expanders and vacuum pumps, are well known in the art. Intraditional scroll device there is a set of scrolls including one fixedscroll and one orbiting scroll making circular translation, orbitingmotion, relative to the former to displace fluid. In a floating scrolldevice there are two sets of scrolls, front and rear scrolls. Each setof scrolls, front or rear, consists of a fixed scroll and an orbitingscroll. Floating scroll technology adopts dual scroll structure. FIG. 5Ais a perspective view of the external appearance of a floating scrollexpander 8. FIG. 5B is an exploded view of the expander 8 of FIG. 5Awhich shows the internal orbiting scroll of floating scroll expander.

Referring to FIG. 6 the working principle of the floating scrollexpander is explained. Front fixed scroll 601 and rear fixed scroll 604are engaged with front orbiting scroll 602 and rear orbiting scroll 603,respectively. The front and rear orbiting scrolls of the dual scroll arearranged back to back and orbit together and can make radial movementrelative to each other during operation.

For simplicity, below we will only describe the working principle of thefront scrolls. The working principle of the rear scrolls is similar. Thesteam enters the expander 8 from the inlet port 610 at the center of thefront fixed scroll. The steam is then sucked into the expansion pocketsformed between the scrolls and is expanded during the orbiting motion ofthe scrolls, and finally, discharges through passage 620 and dischargeport 621 at the peripheral portion of the front fixed scroll. There arethree substantially similar and uniformly distributed crankshafts (onlyone 630 is shown). The crankshafts serve three functions: driving,anti-rotation and axially compliant. The one or more crankshafts convertthe orbiting motion of the orbiting scroll in to rotation and then drivea generator to produce electricity. The three crankshafts work togetherto prevent the orbiting scroll from rotation. The crankshafts also allowthe orbiting scroll move axially, so called the axial compliance, tomaintain the radial seal between the tips and bases of the scroll.

Referring to FIG. 6, the front and rear orbiting scrolls 602 and 603have front end plate 631 and 632, respectively. There is a plenumchamber 633 formed between the two end plates. Sealing element 634 sealsoff plenum chamber 633 from surrounding low-pressure area. The plenumchamber 633 is connected to a selected position of expansion pocketformed between the fixed and orbiting scrolls through a passage 635. Theforces of the steam acting on the area in the plenum chamber 633slightly exceed the total axial forces acting on the opposite surface ofthe front orbiting scroll 602 by the expanding steam. The net axialforces will urge the front orbiting scrolls towards the front fixedscrolls to achieve very light contact between the tips and bases of themating scrolls 601 and 602. This axial compliant mechanism enables agood radial sealing between expansion pockets and makes the wear betweenthe orbiting and fixed scrolls negligible and self-compensating.

In the floating scroll, a crankshaft synchronizer 636 is used to keepthe orientation of three crankshafts being synchronized. Therefore theorbiting scroll is capable to move in the radial direction and keepflank-flank contact of the spiral walls of the mating scrolls. This isso called radial compliance, which enables good tangential seal betweenexpansion pockets formed between mating scrolls.

The axial and radial compliant mechanisms enable the orbiting scrollsdynamically being balanced, yet lightly contacting mating fixed scrollto achieve good and lasting seal for high efficiency and durability. Wecalled it floating scroll technology.

FIG. 7 shows the steam to water exchanger (Co Generator Steam condenser)10 for the embodiment of FIG. 1. The invention uses a plate finexchanger to extract heat from the exhaust of the expander to heat waterfor co generation usages of domestic hot water, heating hot water andother incidental usages. The exchanger 10 can be small in size, but ableto extract all of the co generated hot water that is available, and canbe one manufactured by Alfa Laval model # Tk 205411G01. The exchanger 10allows for fluid flow on one side from expander drive 8 coming in atapproximately 212 to approximately 230 F at approximately 60 psi andgoing out another end to heat dissipation coil 11 and eventually toreturn to heat generator (boiler) 3 The other side of the heat exchanger10 has an opposite flow path with fluid flowing in from co-generationloop 13 (from other loads) and out other end to co-generationrecirculation pump 14 at a temperature of approximately 140 F.

FIG. 8A shows a side view of the steam dissipation coil (heatdissipation steam condenser) 11 for the embodiment of FIG. 1, andincludes a coil and fan assembly FIG. 8B is an end view of the coil andfan assembly of FIG. 8A. The steam dissipation coil provides a method ofcondensing the steam from the expander 8 when all co generated heat hasbeen satisfied. This allows the invention system to continue operatingand providing electricity to the power grid 18 on a 24 hours a day sevendays a week basis. The condensate coil 11 can be manufactured byHeatcraft or other fin and tube manufacturers, and is used for theclosed loop system, and can be made of stainless steel tubes withaluminum fins. The coils 11C allows for dissipation of excess heat whichcannot be utilized in the co-generation loop in FIG. 1.

The heat rejection fan assembly 11F used in the steam dissipationapplication can be a modulating speed motor blower assembly controlledfrom a heat level feed back from the steam dissipation coil. This can bean off-the-shelf fan device of 115 volt, ⅙ horsepower, 1725 RPM with a16-inch propeller fan putting out 1600 CFM at maximum condition. Airflows from the fan 11F through the coils 11C that are about the flowpath lines inside the coil assembly 11.

FIG. 9 shows the configuration of the condensate return pump (highpressure return pump) 5 for the embodiment of FIG. 1. Low pressure fluidcoming from accumulator (water tank) 7 FIG. 1 passes into the metalbellow assembly by line 510. The adjustable eccentric drive expands andcompresses the metal bellows 520 along double arrow E, producing a highpressure output supply of liquid which passes to check valve 6 out line530 back to reclaimer 4 and then to heat generator (boiler) 3 FIG. 1 Afractional electric horsepower motor, M, 560 can be used to rotate anadjustable eccentric wheel drive 550 in the direction of arrow R whichcan be used to expand and compress the metal bellows pump 520 by apiston type connector 540.

This high pressure, low volume pump 5 can provide approximately 600 plusPSI condensate water back into the high pressure boiler supply 3.Bellows pump 5 allows for boiler input conditions greater than or equalto approximately 600 PSI greater than or equal to approximately 200 F,and a mass flow of 95 pounds per hour. Primary description providesseamless high pressure low volume pumping of condensate (steam turnedback to water) in boiler supply circuit (5, 6, 4, 3 FIG. 1).

FIG. 10A shows a top view the air conditioner unit and system 19 forFIG. 1. The A/C module unit 19 can consist of variable speed compressor710, condenser coil 720, refrigerant pump 730, expansion valve 740,evaporator coil 750, variable fan (blower) 760, and variable speed fan(blower) 780. This unit 19 can be a straight A/C unit, not a heat pump,as the heat required by the home will be taken from the cogenerationloop of the invention in FIG. 1.

The air conditioner unit/system 19 can be a high efficiency(approximately 20 SEER) rated to operate on the lowest amount of fuelsource needed. The compressor can either be a straightelectrically-driven compressor or mechanically driven from the expanderdrive 8, and can include:

-   -   1. Refrigerant tubes 790 in the condenser and evaporator can        have rifled interior surfaces with added tube turbulators (see        790X).    -   2. Both condenser and evaporator can have variable fan controls        to match the loads required by the usage.    -   3. The compressor can be an advanced scroll that can be        modulated according to usage needs.    -   4. A liquid refrigerant pump (with Freon) and matched expansion        valve can be used for greater system efficiency.    -   5. A quiet and energy-efficient condenser and evaporator fan        blade can be used. This can be an off-the-shelf item such as one        manufactured by Jet Fan using the Coanda effect.    -   6. A complete model line of approximately 2½ to approximately 5        tons can be available in single and three phase electric input.

The A/C module can have the highest SEER (Seasonal Energy EfficiencyRatio) rating and lowest cost and will be more reliable than anyhigh-efficiency A/C units in the market today. The operation of the A/Cunit and system 19 will now be described in reference to FIG. 10A.

Starting at heat absorbed from the interior environment by theevaporator coil 750. Air from the interior of a space can be blown overthe rifled tube evaporator coil 750 by the variable speed blower (fan)760. The refrigerant (Freon) in absorbing heat has been changed to gas.This low pressure gas continues to the air conditioning variable speedcompressor 710. A suction accumulator (not shown) can be added toprevent liquid from entering the compressor 710. The compressor 710intakes the low pressure heated gas to a high pressure heated gas addingthe heat of compression. This heated refrigerant gas enters the novelrifled tube (detail 790X shown in FIG. 10B), which causes a turbulatedeffect inside tube 790 where ambient air (outside air) induced by thequiet blade fan of blower 780 cools the gas into a liquid. This liquid,under pressure from the compressor 710 is further increased in pressureby a liquid refrigerant (Freon) pump 730 to increase efficiency. Thisliquid then enters a thermal expansion valve 740, where it is expandedthrough an orifice into evaporator 750 removing heat from the interiorenvironment of the space being cooled by A/C unit and system 19 tocomplete the cycle.

FIG. 11 shows a wiring diagram for various components for FIG. 1.Referring to FIGS. 1 and 11, the heat rejection fans used in the steamdissipation coil assembly 11 can be controlled by a modulating speedmotor blower assembly controlled from a heat level feedback from thesteam dissipation coil in the dissipation coil assembly 11. The assembly11 can include a 115 volt, ⅙ horsepower, 1725 RPM with a 16 inchpropeller fan putting out 1600 CFM at maximum condition.

The heat rejecter from the electric generator 9 in FIG. 1 can includes Afractional HP circulator of an antifreeze solution (TACO or Grundfos),115 volts. A pancake blower of 50 CFM (EBM) or similar, 115 volts, witha heat sensitive speed controller (Honeywell) or similar, 115 volts.

Referring to FIGS. 1 and 11, the control module 17, can be anoff-the-shelf product manufactured by Honeywell, Invensys, or Varidigm,and is controlled by a 115 volt input and puts out a 24 volt signalthrough a high limit and switch. This module also controls the gasignition device, either a hot surface igniter or spark igniter of 115volts. Through an internal or external relay it controls the modulatingcombustion blower and modulating gas valve. It also controls the highpressure condensate pump and the electric generator cooling circulatingpump. This pump modulates according to a temperature signal of thecirculating fluid. On separate 115 volt circuits, heat signal modulatingfans control the co generation pump, the dump coil blower fan and thespace heating fan in the air conditioning unit evaporator cabinet. Theair conditioning unit 119 has its own modulation circuit as described inthe air conditioning description previously described.

FIG. 12 shows a perspective view of a preferred layout of all thecomponents of the invention in an approximately 3′ by approximately 4′by approximately 5′ box for use by the end user of the invention.

FIG. 13 shows a second preferred embodiment 1000 for heat generationusing a closed loop steam generator system 1200, 1400, 1500, 1600, 1700.The steam generator (boiler 8) 1100 referenced above in FIGS. 2-3 turnswater into steam by burning a fuel source (22 FIG. 1) such as naturalgas, propane, and any vaporous fuel. Generated steam having atemperature of approximately 280 to approximately 1000 degrees, and apressure range of approximately 100 to approximately 600 psi. Thegenerated steam has an efficiency rating of turning water into steam ofup to approximately 98%, with flue gases being up to the remainingapproximately 2%. The steam enters a steam to water condenser exchanger1200 (10 FIG. 7) where the steam is changed back to water back into theheat (steam) generator by high pressure condensate return pump 1300 (5FIG. 9).

Operation of novel closed loop heat cycle. From the condenser heatexchanger 1200 water passes to hot water circulator 1400 (such asoff-the-shelf water pump) to supply domestic hot water 1500 (through adomestic hot water type heater) at temperature ranges of approximately120 to approximately 140 F. Additionally, the pump 1400 supplies the hotwater to home and/or space heating 1600 (such as but not limited toradiator, base board, radiant in-floor heating pipes, or forced air orhot water/forced air systems) at similar temperatures). Additionally,other heating loads 1700, such as but not limited to pool heating, spaheating, underground pipes for snow/ice removal, and the like. Afterwhich the water is returned to condenser heat exchanger 1200 at a lowertemperature of approximately 20 to approximately 30 degrees lower thanthe outgoing heated water temperature passing through hot watercirculator pump 1300.

The preferred layout of FIG. 17 achieves up to an approximate 98 percentefficiency while standard safety codes (ASTME, American Society ofTesting Material Engineers) has codes of up to the 70 to 80 percentranges. Additionally, the layout can be sized to be fit into a space ofless than 2 by 1 by 1 foot space.

The simplicity and reduced parts in the system of FIG. 17 is cancontinuously run 24 hours a day seven days per week up to approximately50,000 hours or more before any maintenance is needed, and does notrequire any lubrication for the system.

FIG. 14 shows a third preferred embodiment 2000 for powering anair-conditioner unit using the novel steam generator 2100, expander 2400(8 FIGS. 5A, 5B, 6) and steam condenser 2200 of the invention, which isa vaporous fuel supplied air conditioner. The steam generator 2100referenced above in FIGS. 2A-2B turns water into steam by burning a fuelsource such as natural gas, propane, and any vaporous fuel. Generatedsteam having a temperature of approximately 280 to approximately 1000degrees, and a pressure range of approximately 100 to approximately 600psi. The generated steam has an efficiency rating of turning water intosteam of up to approximately 98%, with emitted flue gases being up tothe remaining approximately 2%. The steam enters expander drive 2400(described above in reference to FIGS. 5A, 5B, and 6), which rotatesoutput driveshaft 2450 which is mechanically connected to a direct drivecompressor 2510 such as but not limited to a Copeland Inc. shaft drivencompressor, a Tecumseh Inc. shaft driven compressor, and the like. Theshaft driven compressor 2510 is connected to standard components in astandard airconditioning unit 2550 (fan, condenser and motor forsupplying cooled air), such as but not limited to those manufactured byTrane, York, Carrier, and the like. Compressor 2510 and airconditionerunit 2550 can be held in a single housing 2500.

Steam exiting the Expander drive 2400 passes to a steam to water/aircondenser exchanger 2200 (10 FIG. 7) where the steam is changed back towater back into the heat (steam) generator 2100 (boiler 8 FIGS. 2A, 2B)by high pressure condensate return pump 2300 (5 FIG. 9).

The preferred layout 2000 of FIG. 18 achieves up to an approximate 98percent efficiency of the combined expander, steam condenser and steamgenerator, and these components can fit into a space of less than 3 by 1by 1 foot space. The simplicity and reduced parts in the system of FIG.18 is can continuously run 24 hours a day seven days per week up toapproximately 50,000 hours or more before any maintenance is needed, anddoes not require any lubrication for the system.

FIG. 15 shows a fourth preferred embodiment 3000 for supplyingelectricity to any electrically powered device or system using the novelsteam generator 3100 (boiler 8 FIGS. 2A, 2B), expander drive 3400 (8FIGS. 5A, 5B and 6) and steam condenser 3200 of the invention. The steamgenerator 3100 referenced above in FIGS. 2A-2B turns water into steam byburning a fuel source 22 such as natural gas, propane, and any vaporousfuel. Generated steam having a temperature of approximately 280 toapproximately 1000 degrees, and a pressure range of approximately 100 toapproximately 600 psi. The generated steam has an efficiency rating ofturning water into steam of up to approximately 98%, with emitted fluegases being up to the remaining approximately 2%. The steam entersexpander drive 3400 (described above in reference to FIGS. 5A, 5B and6)), which rotates output driveshaft 3450 which is mechanicallyconnected to an shaft driven electrical generator 3500 such as but notlimited to SmartGen 70-32 W Generator by Light Engineering Inc.,Marathon Generator, e-Cycle Generator, and the like.

Steam exiting the Expander drive 3400 passes to a steam to water/aircondenser exchanger 3200 (10 FIG. 7) where the steam is changed back towater back into the heat (steam) generator 3100 by high pressurecondensate return pump 3300 (5 FIG. 9).

The preferred layout of FIG. 19 achieves up to an approximate 98 percentefficiency of the combined expander, steam condenser and steamgenerator, and these components can fit into a space of less than 3 by 1by 1 foot space.

The simplicity and reduced parts in the system of FIG. 19 cancontinuously run 24 hours a day seven days per week up to approximately50,000 hours or more before any maintenance is needed, and does notrequire any lubrication for the system.

FIG. 16 shows a fifth preferred embodiment 4000 for supplying electricalpower to an electric vehicle 4600, such as an electric car using thenovel steam generator, expander and steam condenser of the invention.The steam generator 4100 referenced above in FIGS. 2A-2B turns waterinto steam by burning a fuel source 22 such as natural gas, propane, andany vaporous fuel. Generated steam having a temperature of approximately280 to approximately 1000 degrees, and a pressure range of approximately100 to approximately 600 psi. The generated steam has an efficiencyrating of turning water into steam of up to approximately 98%, withemitted flue gases being up to the remaining approximately 2%. The steamenters expander drive 4400 (described above in reference to FIGS. 5A, 5Band 6), which rotates output driveshaft 4450 which is mechanicallyconnected to an shaft driven electrical generator 4500 such as but notlimited to SmartGen 70-32 W Generator by Light Engineering Inc.,Marathon Generator, e-Cycle Generator, and the like.

The electric generator 4500 can supply electricity to a vehicle battery4610 which can be connected to electric motors 4620, 4630, 4640, 4650that rotate axles about wheels 4625, 4635, 4645, 4655 of a vehicle 4600such as a car, and the like.

Steam exiting the Expander driver 4400 passes to a steam to water/aircondenser exchanger 4200 (10 FIG. 7) where the steam is changed back towater back into the heat (steam) generator by high pressure condensatereturn pump 4300 (5 FIG. 9).

The preferred layout 4000 of FIG. 20 achieves up to an approximate 98percent efficiency of the combined expander, steam condenser and steamgenerator, and these components can fit into a space of less thanapproximately 3 by approximately 1 by approximately 1 foot space

The simplicity and reduced parts in the system of FIG. 21 cancontinuously run 24 hours a day seven days per week up to approximately50,000 hours or more before any maintenance is needed, and does notrequire any lubrication for the system.

FIG. 17 shows a sixth preferred embodiment 5400 for powering a driveshaft driven vehicle using the novel steam generator 5100, expanderdriver 5400 and steam condenser 5200 of the invention. The steamgenerator 5100 referenced above in FIGS. 2A-2B turns water into steam byburning a fuel source 22 such as natural gas, propane, and any vaporousfuel. Generated steam having a temperature of approximately 280 toapproximately 1000 degrees, and a pressure range of approximately 100 toapproximately 600 psi. The generated steam has an efficiency rating ofturning water into steam of up to approximately 98%, with emitted fluegases being up to the remaining approximately 2%. The steam entersexpander driver 5400 (described above in reference to FIGS. 5A, 5B and6), which rotates output driveshaft 5450 which is mechanically connectedto a drivetrain/axle or which rotates an axle to a wheel(s) 5500 on avehicle 5000 such as a car, and the like.

Steam exiting the Expander driver 5200 passes to a steam to water/aircondenser exchanger 5200 (5 FIG. 7) where the steam is changed back towater back into the heat (steam) generator 5100 by high pressurecondensate return pump 5300 (7 FIG. 9).

The preferred layout 5000 of FIG. 21 achieves up to an approximate 98percent efficiency of the combined expander, steam condenser and steamgenerator, and these components can fit into a space of less than 3 by 1by 1 foot space.

The simplicity and reduced parts in the system of FIG. 21 is cancontinuously run 24 hours a day seven days per week up to approximately50,000 hours or more before any maintenance is needed, and does notrequire any lubrication for the system.

The invention can also use other heat recovery techniques and methods tomaximize energy efficiency. For example, Thermal Photo Voltaic (TPV)devices can also be used with the invention to enhance energyefficiency. The TPV's generate electrical power from heat. TPVs can beinstalled on the exterior surface of an appropriate temperate surface ofdevices such as the system pumps, blowers (fans), and the like, and theelectrical power generated (≈5 W/cm²) will help satisfy parasiticelectrical losses in the invention further increasing efficiency.

Although the invention as been described using a scroll expander driveas the prime mover, other devices such as reciprocating pistons,Wankle-type engines, turbines, and the like can also be utilized to makethe invention work.

Supertropic Power Production Embodiments

As previously mentioned in the background section of this invention,steam engine techniques such as those described in patents by JamesWatts do not solve all the problems of the wasteful energy conversionmethods and systems currently being used.

If we now consider isentropic expansion under the above mentionedconditions of Watt's experiments, we get Full load work and Isentropicexpansion work as:

1. Full load work over the first stroke-meter: approximately 75kps/approximately 1.7 m3/kg=approximately 44 kJ/kg

2. Isentropic expansion work over the remaining 3 stroke-meters: (as persteam properties): 225 kJ/kg,

,where kps″ refers to Kilograms per second; m3/kg″ refers to Kilogramsper cubic meter, and kj/kg″ refers to Kilograms per Kilojoule.

Thus in total: 44 kJ/kg+225 kJ/kg=269 kJ/kg, which is 269/128=2.1 timesmore than without expansion.

As described in the background section of this invention, Watt measureda work factor of approximately 2.4, which thus clearly indicatessupertropic expansion!

In addition, it is important to mind that the above calculation is anideal one (math only computation), whereas Watt's measured values werepractical ones (Actual test data of materials and imperfections inmanufacture), thus showing less than the ideal values for supertropicexpansion.

The work done well over 200 years ago in Watt's time was neverrecognized, because the properties of steam and the physics ofthermodynamics were not known to the present extent, non-condensingsteam engines soon took over from Watt's atmospheric engine and Watt'sexperiments were not recalled by later researchers developing steamtables, ph-diagrams, etc. Also, the estimated gain (supertropicexpansion) was not realized in Watt's days. Losses by friction, byconduction and radiation of heat and by condensation on the cylinderwalls and re-evaporation thereof in the cylinder, of which losses thelatter are most serious.

To achieve supertropic expansion in a displacement system and by virtueof the properties of ammonia, (being a preferred medium), a low pressuresink below atmosphere is needed. As ammonia is very strongly absorbed bywater, such low pressures can easily be obtained by connecting theexpander exhaust to a water-containing vessel.

In view of the above it is clear though that high demands are placed onthe sealing properties of the expander, as we are looking at pressureratios in the size of order of approximately 1:25 (one part expands totwenty five), possibly higher. It can only be done with the high levelof manufacturing technology existing today, to achieve high rotationalspeeds, that minimize the effects of leakage.

With this concept it would be possible to build smaller machines in therange of tenths to hundreds of kilowatts, converting heat of anyexternal source into electrical power. As ammonia is a gas atatmospheric conditions, it can be made to evaporate by absorbing ambientheat, or any low quality heat, such as for the purpose of waste heatrecovery. Thus, the obtained saturated vapor can be superheated with ahigh-quality heat source and the total of energies is than convertedinto mechanical energy.

Depending on the mechanical and specific volumetric properties of anexpander, efficiencies close to ideal, or even over Carnot, can thus beachieved. Carnot would be efficiency defined as the difference of theentering hot temperature minus the leaving cold temperature divided bythe entering hot temperature in Rankine degrees relating to absolutetemperature.

A prime condition for a gas to deliver mechanical energy is a change involume. If the volume remains constant (isochore process), onlytemperature and pressure can change, but no work is done on theboundaries of the system. In thermodynamics three other basic modes ofchange of condition of a gas are considered, which are illustrated inthe TS-diagram (temperature-entropy) shown in FIG. 19A. Different modesare shown for expansion of a trapped gas from volume V1 to V2. Thepressure of the environment (atmospheric) is P2. In FIG. 19A Temperatureis on the vertical axis and entropy is on horizontal axis, and units canbe arbitrary and be any measure of temperature and any unity of entropy.A description of FIG. 19A is listed below.

-   -   1) Isotherm A-B: During the expansive change of volume, work is        done on the boundaries of the system, which at any moment in        time is the same amount of heat energy being applied. Thus the        internal energy remains constant and so does the temperature.        The amount of applied (heat) energy is represented by the        rectangular area A-B-S3-S1    -   2) Isentropic A-D (called “adiabatic” in the PV-diagram): During        the expansive change of volume, work is done on the boundaries        of the system, but no heat is exchanged with the environment.        This means that all the work will be taken from the internal        energy of the gas. As a result, temperature and pressure go        down. The entropy remains unchanged, from which the name        “isentropic”. The according amount of energy is the area under        the V2-curve D-B-S3-S1. If T1 is at ambient temperature, this        amount of energy will be absorbed as latent heat from the        environment, by which the system's condition changes to D, to        restore its original internal energy. This is why an air motor        gets cold.    -   3) Polytropic A-C: If during the expansion an amount of heat        (less than the isotherm amount) is applied, the internal energy        will not decrease as much as in the isentrope case, because part        of the work done comes from this applied heat. This heat is        represented by the area A-C-S2-S1. The total work is represented        by the sum of that area and the area C-B-S3-S2 (latent heat).        Polytropically shifted change of condition is the practical case        in all applications. This is why a compressor gets hot.

If during expansion heat would be cooled off instead, and because theend volume of expansion, V2, remains unchanged, the end of expansionwill then be on a lower temperature, T3 (less internal energy) and lowerpressure P3, which is below the counter pressure P2. Hence, in the endpart of expansion, the environment (P2) will do (negative) work on thesystem boundaries instead and so the total work done by the system willdecrease, with the amount of cooled-off heat, represented by the areaA-S1-So-E.

However, instead of cooling off heat during expansion, the same changeof condition can be achieved by lowering the counter pressure on theworking boundaries (below P3—not shown), thus increasing the workingforce over these boundaries and thus increasing the work that the systemdoes on them. If the end condition of the expanded gas is the same aswould have been by cooling off a certain amount of heat, then theaccording amount of heat energy must have appeared as mechanical work,represented by the area A-S1-So-E. The total mechanical work done by thesystem then is the sum of this and the isentropic work D-B-S3-S1.

FIG. 19B shows a pressure versus Enthalpy graph for the invention.Referring to FIG. 19B, state point (1) is the ammonia vapor that comesout of the desorber (approximately 100 CE at approximately 5 bar),superheated already, and is then further superheated to state point (2)to approximately 300 CE and approximately 2200 kj, where it enters theexpander. In the expander the vapor expands supertropically to statepoint (3) at approximately −61 CE. The green curves are those ofconstant volumity and as such relate directly to the maximum and minimumvolumes of the expander's displacement. The expansion likely will notfollow the straight line between state points (2) and (3), but whateverother path it will follow in practice is totally indifferent, as long asthe expansion ends in state point (3).

If the lowest, end-expansion pressure in the expander is not the same asthe counter pressure from the absorber, it naturally will be higher andthen the expansion will end somewhere on the lower volumity line (v=2.0)at the right of state point (3). It cannot be anywhere else, because theexpander is a displacement machine and thus the end volumity is givenper design. The further the end state point of expansion shifts to theright, the lower the expander shaft output will be, but there is still aLONG way to go until it would reach the intersection for isentropicexpansion (3 a), as shown above. We also see from this that isentropicexpansion is a “hopeless case” to achieve your goal of 45+ percentefficiency.

In state point (3) we see that the volumity line intersects thehorizontal for approximately 0.2 bar at x=0.4 (yellow line), meaningthat approximately 40% of the mass is in gaseous condition and hence,approximately 60% in liquid. The enthalpy of the liquid shows in statepoint (4), approximately −80 kJ/kg, and that of the vapor in state point(5) approximately 1375 kJ/kg. Mind that the enthalpies in the diagramabove are per kilogram of mass, so the actual enthalpies must becorrected for the respective masses (approximately 550 kJ for vapor andapproximately −50 kJ for liquid). The vapor at state point (5) entersthe absorber and we can forget about that part, as far as the ph-diagramis concerned.

The liquid in state point (4) is in the receiver, from where it ispumped to the heat exchanger in the absorber, bringing it to thedesorber pressure of approximately 5 bar—state point (6). Why I havechosen 5 bar, I will explain in my final report. The pump energy, smallas it is, is neglected here (ideal case). With this pressure it entersthe heat exchanger in the absorber, where it is heated to state point(7). We see that x˜ approximately 0.51 there, so around half of theliquid has evaporated already and the whole mixture is saturated ataround approximately 6 CE. Some superheat will occur and gives thelowest temperature of the regenerator at approximately 10 CE and thus isthe temperature of now weak solution, injected in the absorber. It isdriven by the pressure difference between desorber and absorber and aflow-regulating device will be needed to adjust the mass flow. In theregenerator the liquid evaporates further and the resulting vaporsuperheats to finally reach state point (1) at 100 CE, where it joinsthe vapor coming out from the desorber and the cycle is closed.

The beauty of the whole cycle is that there is no designed exchange ofheat with the environment, so, regardless whatever different a practicalsystem might operate from the theoretical one, the energy conversionwill and MUST ALWAYS be 100% in the ideal case (If continuously moreheat is applied than can be converted in the expander, the system willoverheat to destruction).

If the expanding gas is a saturated vapor, it will then becomes wetter(condense more) during supertropic expansion, to deliver the extra work.Water vapor (steam) is not very suitable for this, because itsvaporization enthalpy is very high and so not much of its mass willcondense. Ammonia vapor has about half of the enthalpy of steam and onecould achieve a much more favorable mass ratio between saturated liquidand vapor (60 mass % liquid is possible to achieve). The resultantenergy then would appear as torque on the shaft of the positivedisplacement device, (expander). A preferred goal is to have the endstate of supertropic expansion reach as far as possible in the wet areaof the ph-diagram. In FIG. 20, an exemplary approach is shown. This isnot the only way the final machine can be built, but the functions ofits details are as shown here.

FIG. 20 shows an operational arrangement configuration 7000 for asupertrope power system. The main function of absorber 6600 is toachieve a low pressure, as a condenser normally would do. This lowpressure will instead cause supertropic condensation to occur in theexpander 6400 that thus MUST be a positive displacement type, with afixed expansion ratio.

Similar to the preceding embodiments, the expansion can be a rotarysliding vane machine, scroll expander, or an arrangement withreciprocating pistons, and the like. The components of FIG. 20 will nowbe described.

Heat supply 6100 can be an Alfa Laval or RSI thermal generator burning agaseous fuel.

Superheater 6200 can be a RSI or Alfa Laval that Heats gaseous ammoniato approximately 700 F.

Desorber 6300 can be an Alfa Laval Desorber.

Regenerator 6700 can be a heat exchanger, that takes waste heat forreuse, such as but not limited to a Alfa Laval Flat Plate HeatExchanger.

Receiver 6900 can be a stainless Steel tank that collects ammonia gasand liquid

Absorber 6600 can be Alfa Laval absorber that is used to drop pressureby chemosorption

Pumps 6650 and 6950 can be Cat pump which can be used for pumping liquidammonia.

Exhaust 6350 passes exhaust to the atmosphere or to a co-generation heatexchanger.

Shaft 6450 connects expander 6400 to an alternator 6500, such as anelectric generator from Lite Engineering. The alternator 6500 can supplyelectrical power to various embodiments such as those described in theprevious invention embodiments, such as being used to provide powerelectrical grids, and for supplying all electrical energy and heat needsof a single residential house, commercial business or office building,as well as to a vehicle such as a car, and the like.

In FIG. 20, the desorber 6300 can contain saturated aqua ammonia and isheated to release superheated ammonia vapor at a pressure that iscontrolled per design of the expander 6400. The temperature in thedesorber 6300 should be well below that of evaporation of water, tominimize water evaporation. Any water vapor that follows with theammonia gas, will deliver some work in the expander 6400. As long as itdoesn't interfere with supertropic condensation of the ammonia, no harmis done; otherwise an additional separating device can be used. Anadditional separating device can include but is not limited to anadditional heat exchanger, which used for converting combustion gassesto ammonia gas.

The vapor is superheated further, as shown (to increase the thermalefficiency of the applied heat and the total power output) and thenenters the expander 6400 to drive it. The expander 6400 will discharge amixture of liquid ammonia and ammonia vapor at very low temperatures(around approximately 50 Celsius), that first will be collected in thereceiver 6900, which is connected to the absorber 6600. The dischargedvapor is then fed from the receiver 6900 to the absorber 6600, which byabsorbtion of the vapor creates an under pressure of aroundapproximately 200 mbar, which is “seen” by the expander 6400 discharge.This corresponds with 60 Celsius for saturated water and so the injectedwater at the top of the absorber 6600 should be well below thattemperature, as it will be heated by the exothermic absorbtion process.

To achieve this, the cold ammonia liquid in the receiver 6800,containing a lot of latent energy, could be pumped through a heatexchanger that can cool warm and ammonia-poor water from the desorber6300, prior to it being sprayed into the absorber 6600 (the lowerpressure there will draw it in). In the process, the liquid ammoniaevaporates at a high enough pressure to join the feed vapor from thedesorber 6300 and so it enters the expander again. In this manner theabsorbtion heat is largely recovered (the rest is contained in theenriched, warmed-up water at the bottom of the absorber and will bepumped into the desorber 6300, approximately 100% total recovery, unlessthe absorber 6600 needs additional cooling to ambient.

The enriched water (aqua ammonia), collected in the bottom of theabsorber 6600 is pumped back by pump 6650 into the desorber 6300 and thecycle is closed. The flow-through of the recycling pump 6650 should bechosen as such, that the temperature in the absorber 6600 does notexceed the evaporation level for the water there (approximately 60 C atapproximately 200 mbar), which of course also depends on the coolingcapacity of the liquid ammonia. A control device, such as but notlimited to a simple float switch in the absorber can be used to controloff and on of pump 6950, and can assure that the amount of water sprayedinto the absorber, is the same as the flow-through of the recycle pump(easiest done with a level switch in the absorber, so the pump 6650 canbe over dimensioned).

A chemosorption process is characterized by equilibrium betweenabsorption and desorption. Pressure and temperature decide in whatdirection the process will go, resulting in different concentrations. Iftemperature and pressure would be the same for absorption anddesorption, the concentrations would be the same in both.

Absorption refers to a physical bond and chemosorption to a chemicalbond. Both types of bonding are associated with the generation of heat(absorbtion heat). Absorption is an exothermic reaction (it gives ofheat) and desorption is an endothermic one (it takes up heat). Bychemosorption, ammonia gas reacts with water by forming positiveammonium ions (NH4′) and negative hydroxide ions (OH′) as follows inequation I.NH₃(g)+H₂0(aq)^(H)NH4′(aq)+OH″(aq)±33.6[kJ/mol NH₃]The suffix (g) stands for gaseous condition and (aq) for aqueoussolution.

The total absorption heat for approximately 1 kg of ammonia isapproximately 2180 kJ. This amount of energy must be the same forabsorption and desorption, because it follows from the First Law ofThermodynamics, where Energy can not be created nor destroyed, as isknown by those familiar with basic thermodynamics saying that if asystem is brought into one condition, by adding energy to it, the sameamount of energy must be released by bringing it back into the originalcondition. If there would be a difference, energy would be created fromnothing, or disappear into nothing.

Referring to FIG. 20, air enters combustion blower mixed with a gaseousfuel to a combustion burner. The combustion products 6100 heat ammoniain the finned tubes of the superheater section 6200. The ammonia isheated to approximately 300 C at 5 bar. Q3 (approximately 500 KJ). Thisheated; pressurized ammonia liquid (approximately 5 bar, approximately300 C, volume, approximately 58 M3/kg at approximately 2200 KJ) nowenters the expander 6400, (Scroll, Vane or other positive displacementdevice).

This expander increases the volume to approximately 3.6 times itsoriginal input, (1:3.6). As the volume expands and the temperature dropsto minus approximately 70 F, work is accomplished at the expander shaftand is transferred to the Alternator 6500 as work approximately 1700 KJ.

This shaft 6450 is hermetically sealed from ambient air conditions by amagnetic seal device, well known in the sealing trade. (Ferrofluidics).The shaft rotation is connected to a highly efficient electric generator(Alternator) 6500 producing A/C or D/C electric current. This liquidleaves the expander as Q4 (volume 2 M3/KG and approximately 500 KJ) andis collected in a receiver 6900. This is a mixture of approximately 60%liquid and approximately 40% vapor (approximately 60 M %).

This liquid is pumped by pump 6950 to the Absorber 6100 loosingapproximately 50 KJ. Temperature is minus approximately 60 C. Theammonia gas from the top of the receiver 6900 at approximately 40 M %,at approximately 0.2 bar and minus approximately 61 C providesapproximately 550 KJ to the absorber 6100 shell.

The supertopic effect, created by the mixture of water and ammonia inthe absorber section 6100, creates a low pressure of approximately 0.2bar, allows the temperature to drop from the expander 6400 to minusapproximateley −61 C at approximately 0.2 bar. This allows the expanderto work in a temperature differential of approximately 361 C. Thispredicts a Carnot efficiency of approximately 0.626 (626%).

This is the key to the supertropic effect created here. A normal Rankinecycle in small equipment is between approximately 10% and approximately25% depending on the temperature differences that can be accepted by themost modern materials (approximately 1100 F to approximately 212 F).Even combined cycle central power plants can only expect approximately44% efficiency before line losses to the end user.

From the receiver 6100 liquid ammonia is pumped by pump 6950, to thebottom of the absorber tank 6100. Some of the ammonia gas thataccumulates at the top of the receiver 6900 is connected by tubing tothe absorber 6100.

The liquid part of the expander discharge is fed into a heat exchangerin the absorber 6100, where it will absorb part of the absorption heat,(a maximum temperature difference of about approximately 110 C. Theother part is taken by the solution being warmed up. The liquid has tobe returned as vapor at desorber 6300 conditions, under pressure fromthe liquid pump 6650, the rest of the latent heat can be used to cooldown the aqueous (water) solution from the desorber thus making it weak(low ammonia in the water ammonia solution) prior to injection into thedesorber 6300.

The ammonia vapor from the expander 6400 and receiver 6900 is fed to theabsorber and will react with the water injected there, addingapproximately 870 KJ or a delta energy of approximately 620 KJ. Weaksolution in water/ammonia spray enters the top of the absorber atapproximately 10 C contributing approximately 50 KJ. (Q7). The remainingabsorption heat, not taken out by the liquid cycle, will increase thetemperature to saturation for water at the absorber. It will do that atany circumstance according to Dalton's law that says the pressure in avessel containing more than one medium, corresponds with the lowesttemperature of the according medium and all partial pressures are added.

The absorption system is self adjusting and will generate either a loweror higher counter pressure on the expander 6400. The weakened solutionat approximately +60 C and approximately 20% ammonia is pumped from theabsorber 6100 to the desorber at M=1.2 liters (Q8). Liquid from theabsorber 6100 is pumped by pump 6950 through the absorber 6100 into theregenerator (Q5) 6700/6800 where the liquid ammonia is heated by thewater flow from the desorber 6300 at approximately 1.2 liters andapproximately 500 KJ (Q6=Q7) through the Regenerator 6700/6800 atapproximately 10 C with approximately 50 KJ (Q7) in the regenerator6700/6800 and is mixed with the ammonia flow from the desorber 6300(approximately 5 bar, approximately 100 C, approximately 680 KJ) (Q2)before entering the superheater 6200 combining Q2, Q5, and Q6.1020+680=1700 KJ where approximately 500 KJ Q3 is added. Approximately2200 KJ leaves the Superheater 6200 to enter the expander 6400.

The purpose of the desorber 6300 is to heat the liquid that is pumped toit by the pump 6650 to separate the water from the ammonia so that onlyammonia as a strong solution can enter the superheater section and beheated to approximately 300 C to complete the cycle. Combustion productsnot completely used in the superheater 6200 continues in a conduit tothe desorber 6300 where this heat separates the water from the ammonia.This leaves the desorber 6300 as approximately 7% ammonia andapproximately 1200 KJ (Q1). The desorber 6300 can be constructed as ashell and tube exchanger of a design well known to the industry. Inaddition ambient air can assist in the desorption action to furtherincrease efficiency of the system in the total energy out divided byenergy in as a fuel utilization efficiency.

As the flue finally exits the system 6350, additional heat exchangerscan be added to extract heat for co-generation used primarily fordomestic hot water generation in residential and commercialapplications. This combustion product heat to water being heated is wellknown in the industry and can be plate fin as manufactured by AlfaLaval.

At supertropic expansion, under the conditions as shown in FIG. 20, theexpander 6400 will discharge a liquid-vapor mixture at approximately −61CE, or approximately 212 Kelvin. The mass ratio is approximately 60% forliquid and thus approximately 40% for vapor, both of course beingsaturated at a pressure of approximately 0.2 bar, or approximately 20kPa absolute. Note, the expansion volume ratio of approximately 3.6 at apressure ratio of approximately 25—not possible with isentropicexpansion!

This low pressure is achieved in the absorber 6600 and is dependent onthe speed of absorption. The faster the absorption occurs, the more massof ammonia can be circulated per unit of time and the larger will thepower output on the expander shaft be. A basic advantage of this processis that approximately 40% of the total mass has to be absorbed.

In absorption refrigerators, the absorbed heat is transferred to theenvironment, because the process usually occurs at above ambienttemperature and there is no other sink below that temperature. Ninety to100% energy conversion occurs in the ideal case. Thus the liquid part ofthe expander discharge is fed through a heat exchanger inside theabsorber 6600, where it will absorb a part of the absorption heat, themax temp differential is around approximately 120 CE. The other part ofthe absorber heat is taken up by the solution being warmed up. As theliquid finally has to be returned as vapor at desorber conditions, therest of its latent heat can be used to cool down aqueous solution fromthe desorber and thus making it weak, prior to injection in the desorber6350. The liquid ammonia cycle is herewith closed.

The ammonia vapor from the expander-receiver 6900 is fed to the absorber6600 and will react with the water injected there. The remainingabsorption heat, not taken out by the liquid cycle, will increase thetemperature to saturation for water at absorber pressure (approximately60 CE for 0.2 bar). It will do that under any circumstance, becauseDalton's Law says that the pressure in a vessel containing more than onemedium, corresponds with the lowest temperature of the according medium.Hence, the absorption system is self-adjusting and will generate eithera lower or higher counter pressure on the expander, which only effectsthe shaft power output, but not the functionality and efficiency of thesystem as a whole (see balance calculations below. The strong solutionfrom the absorber is pumped back to the desorber. Herewith the vaporcycle is closed. The top feed line from receiver 6900 feeds gas toabsorber 6600, while the bottom feed line from receiver 6900 to absorber6600 feeds liquid to the absorber 6600.

FIG. 22 shows an energy balance diagram 8000 for the supertrope powersystem of the invention shown in the previous embodiments, and shows theenergy balance for the process. The process is described below inreference to FIG. 22.

An energy balance exists between the energy inputted and the energy out.

Q1 heat energy entering the absorber A(8600) 1200 KJ

Q2 heat energy leaving the desorber D(8300 680 KJ

Q3 heat added at the superheater 500 KJ

Work equal Q1+Q3 2200 KJ

Balance Conditions

Desorber in=Q1+Q8 1200 KJ+(−20 KJ) 1180 KJ

Desorber out=Q2+Q6+Q7 680 KJ+450 KJ+50 KJ 1180 KJ

Absorber in=Q4+Q7 500 KJ+50 KJ 550 KJ

Absorber Out=Q5+Q8 570 KJ+(−20) KJ 550 KJ

Expander (8400) in=Q2+Q6+Q5+Q3 680 KJ+450 KJ+570 KJ+500 KJ 2200 KJ

Expander (8400) out=Q4 500 KJ+Work Q1+Q3 (1700 KJ) 2200 KJ

Expander (8400) in-expander out Q2+Q5+Q5+Q3−Q4=W=Q1+Q3 1700 KJQ1=Q2+Q6+Q5−Q4  (3)Desorber (8300) in-Desorber (8600) out=Q1+Q8−Q2−Q6−Q7 (4)=0(3) & (4) combined eliminating Q1—Desorber in-Desorber out=Q5−Q4+Q8−Q7(5)=0

(Absorber in-Absorber out)=Q5−Q4+Q8−Q7 (6)=0

Energy Balance from Q's and W on FIG. 21

Energy balance requires that Ain=Aout and thus Q4+Q7=Q5+Q8 which meansQ8=−20 kJ. This value inserted in equations (5) and (6) makes them zero,as required for energy balance. Din=Dout and Q8=−20 kJ, givesQ1=Q2+Q6+Q7−(−20)=1200 kJ.

FIG. 22 shows another version of the supertropic power system 9000 ofthe preceding figures with a gas/air mixture heat source and superheatorbased on forced gas/air combustion. The components of FIG. 22 will nowbe described, and are similar to those previously described in referenceto FIG. 20.

Combustion blower 9100 can be one manufactured by Ametex and EBM.

Gaseous Fuel 9125 can be any gaseous fuel, natural gas, propane, and thelike.

Burner 9150 can be one manufactured by Beckert or RSI.

Blower 9100 can be a fan, and the like.

Superheater 9200 can be a Alfa Laval, MDE superheater.

Desorber 9300 can be an Alfa Laval desorber.

Pumps 9650 and 9950 can be Cat pumps.

Absorber 9600 can be an Alfa Laval absorber.

Regenerator 9700 can be an Alfa Laval regenerator.

Receiver Tank 9900 can be a simple stainless steel tank

20 HP scroll expander 9400 can be a Copeland type expander.

15 KW alternator can be a Lite Engineering motor.

The operation of the system in FIG. 22 is described as follows. Air 9050enters combustion blower 9100, and can be mixed with a gaseous fuel9125, such as natural gas, propane, and the like, to a combustion burner9150. The combustion which can produce heated ammonia in the finnedtubes 9250 of the superheater section 9200. The ammonia can be heated toapproximately 700 F at approximately 75 psi.

This heated, pressurized ammonia liquid now enters the expander 9400,(such as but not limited to a Scroll, Vane or other positivedisplacement device). This expander 9400 increases the volume toapproximately 3.6 times its original input. As the volume expands andthe temperature drops to minus approximately 70 F, work is accomplishedat the expander shaft 9450.

This shaft 9450 can be hermetically sealed from ambient air conditionsby a magnetic seal device, such as but not limited to a Ferro fluidicsseal, and the like. The shaft 9450 rotation can be connected to a highlyefficient electric generator 9500 such as an alternator that waspreviously described producing A/C or D/C electric current.

The liquid leaving the expander 9400 can be collected in a receiver9900, which can be a mixture of approximately 60% liquid andapproximately 40% vapor.

The supertopic effect, created by the mixture of water and ammonia inthe absorber section 9600, can create a low pressure of approximately 3psi, allowing the temperature to drop from the expander 9400 to minusapproximately 70 F. This allows the expander 9400 to work in atemperature differential of approximately 770 F, which predicts a Carnotefficiency of approximately 0.626 (62.6%). The Carnot efficiency can bethe result of (700+460) minus (70+460) divided by (700+460)=0.626 or62.6%

This is the key to the supertropic effect created here. A normal Rankinecycle in small equipment is between approximately 10% and approximately25% depending on the temperature differences that can be accepted by themost modern materials (approximately 1100 F to approximately 212 F).Even combined cycle central power plants can only expect approximately44% efficiency before line losses to the end user.

From the receiver 9900 liquid ammonia can be pumped by pump 9950, to thebottom of the absorber tank 9600. Some of the ammonia gas thataccumulates at the top of the receiver 9900 can be connected by tubing9910 to the absorber 9600.

The liquid part of the expander 9400 discharge is fed into a heatexchanger in the absorber 9600, where it will absorb part of theabsorption heat, (a maximum temperature difference of aboutapproximately 230 F. The other part is taken by the solution beingwarmed up. The liquid has to be returned as vapor at desorber 9300conditions, under pressure from the liquid pump 9950, the rest of thelatent heat can be used to cool down the aqueous (water) solution fromthe desorber 9300 thus making it weak (low ammonia in the water ammoniasolution) prior to injection into the desorber 9300.

The ammonia vapor from the expander 9400 receiver 9900 is fed to theabsorber 9600 and will react with the water injected there. Theremaining absorption heat, not taken out by the liquid cycle, willincrease the temperature to saturation for water at the absorberpressure (approximately 140 F and approximately 3 psi). It will do thatat any circumstance according to Dalton's law that says the pressure ina vessel containing more than one medium, corresponds with the lowesttemperature of the according medium. Daltons law is when the pressure ofa gas mixture is the sum of all the partial gas pressures. Theabsorption system is self adjusting and will generate either a lower orhigher counter pressure on the expander 9400. The strong solution ispumped from the absorber 9600 to the desorber 9300.

Referring again to FIG. 22, liquid from the absorber 9600 can be pumpedby pump 9950 through the absorber 9600 into the regenerator 9700 wherethe liquid ammonia is heated by the water flow from the desorber 9300 inthe reclaimer 9700 and is mixed with the ammonia flow from the desorber9300 before entering the superheater 9200.

The purpose of the desorber 9300 is to heat the liquid that is pumped toit by the pump 9650 to separate the water from the ammonia so that onlyammonia as a strong solution can enter the superheater section 9200 andbe heated to approximately 700 F to complete the cycle. Combustionproducts not completely used in the superheater 9200 continues in aconduit to the desorber 9300 where this heat separates the water fromthe ammonia. The desorber 9300 can be constructed as a shell and tubeexchanger 9325 of a design well known to the industry. In addition,ambient air can assist in the desorption action to further increaseefficiency of the system in the total energy out divided by energy in asa fuel utilization efficiency.

As the flue 9350 finally exits the system 9000, additional heatexchangers can be added to extract heat for co-generation used primarilyfor domestic hot water generation in residential and commercialapplications such as those described previously in this invention. Suchheat exchangers can include, but are not limited to combustion fluegasses to domestic hot water as a plate fin exchanger known to thosefamiliar with the art.

The supertropic power pack can be used to supply electrical power topower grids. The invention embodiments can provide power to allcommercial and residential applications, as well as supply power forrunning vehicles, such as but not limited to electric cars, and thelike.

While the invention has been described, disclosed, illustrated and shownin various terms of certain embodiments or modifications which it haspresumed in practice, the scope of the invention is not intended to be,nor should it be deemed to be, limited thereby and such othermodifications or embodiments as may be suggested by the teachings hereinare particularly reserved especially as they fall within the breadth andscope of the claims here appended.

1. A method of converting moderate amounts of heat into mechanicalenergy at high efficiencies, comprising the steps of: supertropicallyexpanding a gas vapor against a vacuum, as generated by chemosorption,in order to convert moderate amounts of heat into mechanical energy athigh efficiencies.
 2. The method of claim 2, further comprising the stepof: providing ammonia as the gas vapor.
 3. A supertropic energygenerating package system, comprising: a gaseous source; a thermalgenerator for heating the source of ammonia/water and generating a gas;a scroll expander for expanding the gas; and a power source being drivenby the expanding gas, the power source generating electricity therefrom.4. The system of claim 3, wherein the gaseous source includes: ammoniaand water.
 5. A supertropic expansion device, for converting heat intomechanical energy, comprising: means for expanding vapors close to, orbeing at saturation condition against a lower pressure than atmospheric,at polytrophic expansion conditions, as generated otherwise than bysurface condensation.
 6. The device according to claim 5, furthercomprising: means for achieving said polytrophic expansion conditionsinternally in a rotary sliding vane machine.
 7. The device according toclaim 5, further comprising: means for achieving said polytrophicexpansion conditions in a displacement device, by injection of fluidstherein.
 8. A method of generating electrical power from ammonia,comprising the steps of: heating ammonia gas; expanding the heatedammonia by an expander to a larger volume while dropping temperature ofthe ammonia gas; driving a motor by the expander; and generatingelectricity from the motor.
 9. The method of claim 8, wherein theheating step includes the steps of: heating the ammonia to approximately700 F at approximately 75 psi.
 10. The method of claim 8, wherein theexpanding step includes the steps of: increasing the volumne of theheated ammonia gas to approximately 3.6 times its original input whiledropping temperature to minus approximately 70 F.
 11. The method ofclaim 8, wherein the driving step includes the step of: rotating a shaftattached to the motor by the expander.
 12. The method of claim 8,further comprising the step of: providing an alternator as the motor.13. The method of claim 8, further comprising the step of: collectingfluid from the expander in a reservoir
 14. The method of claim 13,wherein the fluid can be a mixture of approximately 60% liquid andapproximately 40% vapor.
 15. The method of claim 13, further comprisingthe step of: passing the liquid and the vapor from the receiver to anabsorber.
 16. The method of claim 15, further comprising the steps of:creating a low pressure in the absorber which allows the temperature todrop from the expander; and causing the expander to work in asubstantial temperature differential for a high Carnot efficiency, andeffecting a supertropic effect therefrom.
 17. The method of claim 16,wherein the low pressure is approximately 3 psi, and the temperaturedrop in the expander is minus approximately 70 F, the temperaturedifferential is approximately 770 F, and the Carnot efficiency isapproximately 62.6%
 18. The method of claim 16, further comprising thestep of: cycling liquid back to the absorber by a desorber to increaseefficiency of the electricity being generated.
 19. A method ofgenerating electrical energy from an expanding gas, comprising the stepsof: heating fluid into a gas; supertropically expanding the gas by anexpander; driving an electric generator by the expander; generatingelectricity from the electric generator; condensing the gas into aliquid; passing the liquid through an absorber, a regenerator, and adesorber in a closed cycle to continuously provide a vacuum conditionfor the supertropic expansion.